Carbon dioxide fractionalization process

ABSTRACT

A method comprises separating a hydrocarbon feed stream having carbon dioxide into a heavy hydrocarbon stream and a light hydrocarbon stream. The light hydrocarbon stream is separated into a carbon dioxide-rich stream and a carbon dioxide-lean stream. At least a portion of the carbon dioxide-lean stream is fed to a hydrocarbon sweetening process. Another method comprises receiving a hydrocarbon feed stream that comprises 30 molar percent to 80 molar percent carbon dioxide. A heavy hydrocarbon stream is separated from the hydrocarbon feed stream, wherein the heavy hydrocarbon stream comprises at least 90 molar percent C3+ hydrocarbons. A carbon dioxide-rich stream is separated from the hydrocarbon feed stream, wherein the carbon dioxide-rich stream comprises at least 95 molar percent carbon dioxide.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. patent application Ser. No.14/200,346, filed Mar. 7, 2014, which is a divisional of U.S. patentapplication Ser. No. 12/824,382, filed Jun. 28, 2010, now U.S. Pat. No.8,709,215, which is a divisional of U.S. patent application Ser. No.11/621,913 filed Jan. 10, 2007, now Reissued U.S. Pat. No. RE 44,462,the contents of all of which are incorporated herein by reference as ifreproduced in their entireties.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

Not applicable.

REFERENCE TO A MICROFICHE APPENDIX

Not applicable.

BACKGROUND

Carbon dioxide is a naturally occurring substance in most hydrocarbonformations. While the carbon dioxide concentration will depend on thelocation of the formation, carbon dioxide concentrations as high aseighty percent are common in many areas, such as West Texas. Moreover,the implementation of tertiary recovery operations, such as carbondioxide injection into the subterranean wellbore, can increase thecarbon dioxide concentration within the produced hydrocarbons. In eithercase, the carbon dioxide concentration of the produced hydrocarbons maybe sufficiently high to require the carbon dioxide concentration to bereduced before the hydrocarbons can be refined or further processed.

Several solutions are known for reducing the carbon dioxideconcentration or “sweetening” a hydrocarbon stream. For example, amineprocesses, physical solvent processes, membrane processes, and carbondioxide recovery processes have all been used to sweeten hydrocarbonstreams. The processing facilities employing these hydrocarbonsweetening processes are generally sized for a specific processingcapacity and hydrocarbon feed stream composition. As such, when thecarbon dioxide concentration of the hydrocarbon feed stream increases oradditional feedstock comes online, then an additional processingfacility must be constructed to compensate for the change in hydrocarbonfeed stream composition or the increased feedstock. The construction ofa new processing facility is undesirable because of the substantialcapital cost, operating costs, and time delay inherent in such asolution.

SUMMARY

In one aspect, the disclosure includes a method comprising separating ahydrocarbon feed stream having carbon dioxide into a heavy hydrocarbonstream and a light hydrocarbon stream. The light hydrocarbon stream isseparated into a carbon dioxide-rich stream and a carbon dioxide-leanstream. At least a portion of the carbon dioxide-lean stream is fed to ahydrocarbon sweetening process.

In another aspect, the disclosure includes a method comprising receivinga hydrocarbon feed stream that comprises 30 molar percent to 80 molarpercent carbon dioxide. A heavy hydrocarbon stream is separated from thehydrocarbon feed stream, wherein the heavy hydrocarbon stream comprisesat least 90 molar percent C₃₊ hydrocarbons. A carbon dioxide-rich streamis separated from the hydrocarbon feed stream, wherein the carbondioxide-rich stream comprises at least 95 molar percent carbon dioxide.

In a third aspect, the disclosure includes a method comprising receivinga hydrocarbon feed stream that comprises carbon dioxide. The hydrocarbonfeed stream is separated into a carbon dioxide-lean stream and a carbondioxide-rich stream. The carbon dioxide-lean stream comprises at least20 molar percent less carbon dioxide than the hydrocarbon feed stream,and the carbon dioxide-rich stream comprises less than 10 molar percenthydrocarbons.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a process flow diagram of one embodiment of the carbon dioxidefractionalization process; and

FIG. 2 is a process flow diagram of another embodiment of the carbondioxide fractionalization process.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

Disclosed herein is a carbon dioxide fractionalization process that maybe positioned in front of an existing hydrocarbon sweetening process toincrease the processing capacity of the hydrocarbon sweetening process.Specifically, the carbon dioxide fractionalization process purifies thehydrocarbon feed stream by removing at least some of the carbon dioxideand the heavy hydrocarbons from a hydrocarbon feed stream. Thepurification of the hydrocarbon stream reduces the carbon dioxide andheavy hydrocarbon loading on the hydrocarbon sweetening process, therebyincreasing the processing capacity of the hydrocarbon sweeteningprocess. Furthermore, the carbon dioxide fractionalization processproduces a carbon dioxide-rich stream that may be injected into asubterranean formation.

FIG. 1 illustrates one embodiment of the carbon dioxidefractionalization process 100. The carbon dioxide fractionalizationprocess 100 separates a hydrocarbon feed stream 200 into a heavyhydrocarbon stream 254, an acid gas stream 250, a carbon dioxide-richstream 244, and a carbon dioxide-lean stream 234, the compositions ofwhich are discussed in detail below. The carbon dioxidefractionalization process 100 receives the hydrocarbon feed stream 200and may pass the hydrocarbon feed stream 200 through a heat exchanger102 that uses the cooled carbon dioxide-lean stream 232 to reduce thetemperature of the hydrocarbon feed stream 200. A first separation unit101 that comprises one or more of a separator 108, a reboiler 110, acondenser 132, and a separator 134 may then remove the heavyhydrocarbons from the cooled hydrocarbon feed stream 202. Specifically,the separator 108 separates the cooled hydrocarbon feed stream 202 intoa bottom effluent stream 208 and a top effluent stream 214. The topeffluent stream 214 may then be fed into a condenser 132, which may giveoff energy 312 by being cooled, and separates the top effluent stream214 into a reflux stream 246 and a light hydrocarbon stream 248.Similarly, the bottom effluent stream 208 may be fed into the reboiler110, which may receive energy 302 by being heated, and separates thebottom effluent stream 208 into a recycle stream 210 and a heavyhydrocarbon stream 212. The heavy hydrocarbon stream 212 may then be fedinto a separator 134 that separates an acid gas stream 250 from theheavy hydrocarbon stream 252. The heavy hydrocarbon stream 252 mayoptionally be cooled by a heat exchanger 114, for example an air cooler,to produce the heavy hydrocarbon stream 254.

Returning to the light hydrocarbon stream 248, the light hydrocarbonstream 248 may be fed into a compressor 112 that receives mechanical orelectrical energy 304 and increases the pressure and/or temperature ofthe light hydrocarbon stream 248, thereby creating a compressed lighthydrocarbon stream 216. The compressed light hydrocarbon stream 216 maythen be fed into a heat exchanger 118 that uses a chilled carbondioxide-lean stream 230 to reduce the temperature of the compressedlight hydrocarbon stream 216, thereby producing a chilled lighthydrocarbon stream 224. A second separation unit 103 that comprises oneor more of a separator 120, a reboiler 124, and a condenser 122 may thenremove at least some of the carbon dioxide from the chilled lighthydrocarbon stream 224. Specifically, the separator 120 separates thechilled light hydrocarbon stream 224 into a heavy effluent stream 236and a light effluent stream 226. The light effluent stream 226 may befed into the condenser 122, which may give off energy 306 by beingcooled, and separates the light effluent stream 226 into a reflux stream228 and the chilled carbon dioxide-lean stream 230. The chilled carbondioxide-lean stream 230 may then be passed through the heat exchangers118, 102 and into a hydrocarbon sweetening process 130. The hydrocarbonsweetening process 130 may be any process that removes carbon dioxidefrom a hydrocarbon stream to make the hydrocarbon stream suitable fortransportation and/or further processing. Persons of ordinary skill inthe art are aware of numerous different hydrocarbon sweetening processes130, as illustrated by Field Processing of Petroleum, Vol. 1: NaturalGas by Manning et al., incorporated herein by reference as if reproducedin its entirety. Several examples of the hydrocarbon sweetening process130 are discussed in detail below.

Returning to the separator 120, the heavy effluent stream 236 may be fedinto the reboiler 124, which may receive energy 308 in the form of heat,and separates the heavy effluent stream 236 into a recycle stream 238and a cooled carbon dioxide-rich stream 240. The cooled carbondioxide-rich stream 240 may optionally be combined with the acid gasstream 250, if desired. The cooled carbon dioxide-rich stream 240 maythen be fed through a heat exchanger 126 that further cools the cooledcarbon dioxide-rich stream 240 by removing energy 310 from the cooledcarbon dioxide-rich stream 240, thereby producing the chilled carbondioxide-rich stream 242. The chilled carbon dioxide-rich stream 242 mayalso be fed to a pump 128 that uses energy 314 to pump the carbondioxide-rich stream 244 to another location, perhaps for injection intoa subterranean formation.

FIG. 2 illustrates another embodiment of the carbon dioxidefractionalization process 100. Similar to the embodiment shown in FIG.1, the carbon dioxide fractionalization process 100 shown in FIG. 2separates the hydrocarbon feed stream 200 into the heavy hydrocarbonstream 212, the carbon dioxide-rich stream 244, and the carbondioxide-lean stream 234, the compositions of which are discussed indetail below. The carbon dioxide fractionalization process 100 receivesthe hydrocarbon feed stream 200 and passes the hydrocarbon feed stream200 through a heat exchanger 102 that uses the cooled carbondioxide-lean stream 232 to reduce the temperature of the hydrocarbonfeed stream 200. After the cooled hydrocarbon feed stream 202 exits theheat exchanger 102, the hydrocarbon feed stream 200 is fed into theoptional heat exchanger 104, which further cools the cooled hydrocarbonfeed stream 202 by removing some of its energy 300, thereby producing acooled hydrocarbon feed stream 202.

A first separation unit 101 that comprises one or more of separators106, 108 and the reboiler 110 may then remove the heavy hydrocarbonsfrom the cooled hydrocarbon feed stream 202. Specifically, the cooledhydrocarbon feed stream 202 may be fed into a separator 106 thatseparates the cooled hydrocarbon feed stream 202 into a light fraction220 and a heavy fraction 206. In an embodiment, the light fraction 220may be a vapor phase and the heavy fraction 206 may be a liquid phase.The light fraction 220 may be combined with the compressed lighthydrocarbon stream 216 in a mixer 116 and the heavy fraction 206 may befed into the separator 108. The separator 108 separates the heavyfraction 206 into a bottom effluent stream 208 and a top effluent stream214. The bottom effluent stream 208 may be fed into a reboiler 110,which may receive energy 302 by being heated, and separates the bottomeffluent stream 208 into a recycle stream 210 and the heavy hydrocarbonstream 212. The top effluent 214 may be fed into the compressor 112 thatreceives mechanical or electrical energy 304 and increases the pressureand/or temperature of the top effluent 214, thereby creating acompressed light hydrocarbon stream 216. The compressed lighthydrocarbon stream 216 may optionally be cooled, for example, by theheat exchanger 114, which may be an air cooler, to produce a cooledlight hydrocarbon stream 218. The cooled light hydrocarbon stream 218may then be mixed with the light fraction 220 in the mixer 116. Theresulting mixed light hydrocarbon stream 222 may then be processed asdescribed above for the compressed light hydrocarbon stream 216 in FIG.1 to produce the carbon dioxide-lean stream 234.

The hydrocarbon feed stream 200 may contain a mixture of hydrocarbonsand carbon dioxide. Numerous types of hydrocarbons may be present in thehydrocarbon feed stream 200, including methane, ethane, propane,i-butane, n-butane, i-pentane, n-pentane, hexane, octane, and otherhydrocarbon compounds. For example, the hydrocarbon feed stream 200 maycontain from about 10 percent to about 60 percent methane, no more thanabout 10 percent ethane, and no more than about 5 percent propane andheavier hydrocarbons (C₃₊). Although the hydrocarbon feed stream 200 maycontain any carbon dioxide concentration, in various embodiments thehydrocarbon feed stream 200 contains from about 10 percent to about 90percent, from about 30 percent to about 80 percent, or from about 50percent to about 70 percent of the carbon dioxide. The hydrocarbon feedstream 200 may also include other compounds such as water, nitrogen,hydrogen sulfide (H₂S), and/or other acid gases. Finally, thehydrocarbon feed stream 200 may be in any state including a liquidstate, a vapor state, or a combination of liquid and vapor states.Finally, unless otherwise stated, the percentages herein are provided ona mole basis.

Similar to the hydrocarbon feed stream 200, the carbon dioxide-leanstream 234 may contain a mixture of hydrocarbons and carbon dioxide.Specifically, the composition of the carbon dioxide-lean stream 234 maycontain an increased methane concentration and a decreased carbondioxide concentration compared to the hydrocarbon feed stream 200. Inembodiments, the carbon dioxide-lean stream 234 contains less than about60 percent, from about 20 percent to about 50 percent, or from about 30percent to about 40 percent of the carbon dioxide. In yet otherembodiments, the carbon dioxide concentration in the carbon dioxide-leanstream 234 is at least about 20 percent, at least about 40 percent, orat least about 60 percent less than the carbon dioxide concentrationpresent in the hydrocarbon feed stream 200. The carbon dioxide-leanstream 234 may also contain a reduced concentration of C₃₊ compared tothe hydrocarbon feed stream 200. In various embodiments, the carbondioxide-lean stream 234 comprises less than about 5 percent, less thanabout 1 percent, or is substantially free of C₃₊. In yet otherembodiments, the C₃₊ concentration in the carbon dioxide-lean stream 234is at least about 20 percent, at least about 40 percent, or at leastabout 60 percent less than the C₃₊ concentration present in thehydrocarbon feed stream 200. Finally, in other embodiments, the carbondioxide-lean stream 234 contains at least about 90 percent, at leastabout 98 percent, or at least about 99 percent of a combination ofmethane and carbon dioxide.

The heavy hydrocarbon streams 212, 252, 254 may contain a mixture ofheavy hydrocarbons and some other compounds. Specifically, thecomposition of the heavy hydrocarbon streams 212, 252, 254 contains anincreased C₃₊ concentration and a decreased methane concentration,ethane, and carbon dioxide compared to the hydrocarbon feed stream 200.In embodiments, the heavy hydrocarbon streams 212, 252, 254 comprises atleast about 90 percent, at least about 95 percent, or at least about 99percent C₃₊. In other embodiments, the heavy hydrocarbon streams 212,252, 254 comprises less than about 5 percent, less than about 1 percent,or is substantially free of methane and/or ethane. In yet otherembodiments, the heavy hydrocarbon streams 212, 252, 254 contains lessthan about 10 percent, less than about 5 percent, or less than about 1percent of the carbon dioxide. Alternatively, the heavy hydrocarbonstreams 212, 252, 254 comprises at least about 20 percent, at leastabout 40 percent, or at least about 60 percent less carbon dioxide thanthe hydrocarbon feed stream 200. In an embodiment, the heavy hydrocarbonstreams 212, 252, 254 described herein are suitable for use or sale asnatural gas liquids (NGL).

The carbon dioxide-rich stream 244 described herein may comprise amixture of hydrocarbons and carbon dioxide. Specifically, the carbondioxide-rich stream 244 contains a decreased concentration ofhydrocarbons and an increased carbon dioxide concentration compared tothe hydrocarbon feed stream 200. In various embodiments, the carbondioxide-rich stream 244 comprises less than about 10 percent, less thanabout 5 percent, or is substantially free of hydrocarbons. In otherembodiments, the carbon dioxide-rich stream 244 contains at least about80 percent, at least about 90 percent, or at least about 95 percent ofthe carbon dioxide. The carbon dioxide-rich stream 244 described hereinmay be vented, transported, sold, or used for other purposes includingreinjection into a subterranean formation.

The acid gas stream 250 described herein may comprise a mixture ofhydrocarbons and at least one acid gas, such as H₂S or carbon dioxide.Specifically, the composition of the acid gas stream 250 may contain adecreased hydrocarbon concentration and an increased acid gasconcentration compared to the hydrocarbon feed stream 200. In variousembodiments, the acid gas stream 250 comprises less than about 10percent, less than about 5 percent, or is substantially free ofhydrocarbons. In other embodiments, the acid gas stream 250 contains atleast about 90 percent, at least about 95 percent, or at least about 99percent of the acid gas. The acid gas stream 250 described herein may bevented, sold, reinjected, or otherwise disposed of as desired.

Although the hydrocarbon sweetening process 130 may be any sweeteningprocess, in one embodiment the hydrocarbon sweetening process 130 is aphysical solvent process. The physical solvent process sweetens thehydrocarbon stream by using an organic solvent to absorb the carbondioxide from the hydrocarbon stream. Examples of these physical solventsinclude SELEXOL®, RECTISOL®, PURISOL®, and FLUOR® solvents such aspropylene carbonate. The physical solvent process begins by contactingthe carbon dioxide-lean stream 234 with the solvent at high pressure.The solvent absorbs the carbon dioxide such that subsequent separationof the solvent from the hydrocarbons produces a hydrocarbon stream witha relatively low carbon dioxide concentration. The carbon dioxide-loadedsolvent is then regenerated by lowering the pressure of the solvent,typically through a series of flash drums, which causes the carbondioxide to separate from the solvent. The solvent is then compressed andrecycled into the hydrocarbon stream, while the carbon dioxide is ventedor sold.

Alternatively, the hydrocarbon sweetening process 130 may be a membraneseparation process. Membrane separation processes use membranes toseparate carbon dioxide from the carbon dioxide-lean stream 234 at themolecular level. Specifically, the pores in the membranes are sized toallow carbon dioxide to pass through the membrane and form a permeategas, while the larger hydrocarbon molecules bypass the membrane and forma residue gas. Depending on the composition of the hydrocarbons, thisconfiguration may be reversed such that the carbon dioxide forms theresidue gas and the hydrocarbons form the permeate gas. Because themembrane process is dependent on, among other factors, the compositionof the hydrocarbons, the selection of the pore size is best determinedby persons of ordinary skill in the art.

In yet another embodiment, the hydrocarbon sweetening process 130 may bea carbon dioxide recovery process. One example of a suitable carbondioxide recovery process is the Ryan-Holmes process. The Ryan-Holmesprocess uses a solvent and a plurality of columns to separate the carbondioxide-lean stream 234 into a carbon dioxide-rich stream, amethane-rich stream, an ethane-rich stream, and a heavy hydrocarbonstream. The columns may include a demethanizer, a carbon dioxiderecovery unit, a propane recovery unit, and a solvent recovery unit. Thecolumns are arranged in series with the solvent being recycled to thefirst column in the series. The specific arrangement of the variouscolumns depends on the composition of the feed hydrocarbon stream and isbest determined by persons of ordinary skill in the art. Finally,persons of ordinary skill in the art will appreciate that thehydrocarbon sweetening process 130 may be a process other than theexemplary processes described herein.

When the carbon dioxide fractionalization process 100 is implementedprior to a hydrocarbon sweetening process 130, the processing capacityof the hydrocarbon sweetening process 130 is increased. Specifically,the processing capacity of the hydrocarbon sweetening process 130 may bedirectly proportional to the decrease in carbon dioxide concentrationbetween the hydrocarbon feed stream 200 and the carbon dioxide-leanstream 234. For example, if the carbon dioxide concentration of thecarbon dioxide-lean stream 234 is half of the carbon dioxideconcentration of the hydrocarbon feed stream 200, then the processingcapacity of the hydrocarbon sweetening process 130 is doubled. Inaddition, the processing capacity of the hydrocarbon sweetening process130 may be directly proportional to the decrease in flow rate betweenthe hydrocarbon feed stream 200 and the carbon dioxide-lean stream 234.For example, if the flow rate of the carbon dioxide-lean stream 234 ishalf of the flow rate of the hydrocarbon feed stream 200, then theprocessing capacity of the hydrocarbon sweetening process 130 is alsodoubled. The two affects may also be cumulative such that if the carbondioxide concentration of the carbon dioxide-lean stream 234 is half ofthe carbon dioxide concentration of the hydrocarbon feed stream 200 andthe flow rate of the carbon dioxide-lean stream 234 is half of the flowrate of the hydrocarbon feed stream 200, then the processing capacity ofthe hydrocarbon sweetening process 130 is increased by a factor of four.

The separators 106, 108, 120, 134 may be any of a variety of processequipment suitable for separating a stream into two separate streamshaving different compositions, states, temperatures, and/or pressures.For example, one or more of the separators 106, 108, 120, 134 may be acolumn having trays, packing, or some other type of complex internalstructure. Examples of such columns include scrubbers, strippers,absorbers, adsorbers, packed columns, and distillation columns havingvalve, sieve, or other types of trays. Such columns may employ weirs,downspouts, internal baffles, temperature, and/or pressure controlelements. Such columns may also employ some combination of refluxcondensers and/or reboilers, including intermediate stage condensers andreboilers. Alternatively, one or more of the separators 106, 108, 120,134 may be a phase separator. A phase separator is a vessel thatseparates an inlet stream into a substantially vapor stream and asubstantially liquid stream, such as a knock-out drum or a flash drum.Such vessels may have some internal baffles, temperature, and/orpressure control elements, but generally lack any trays or other type ofcomplex internal structure commonly found in columns. Finally, one ormore of the separators 106, 108, 120, 134 may be any other type ofseparator, such as a membrane separator.

The reboilers 110, 124 and condensers 122, 132 described herein may beany of a variety of process equipment suitable for changing thetemperature and/or separating any of the streams described herein. Inembodiments, the reboilers 110, 124 and the condensers 122, 132 may beany vessel that separates an inlet stream into a substantially vaporstream and a substantially liquid stream. These vessels typically havesome internal baffles, temperature, and/or pressure control elements,but generally lack any trays or other type of complex internal structurefound in other vessels. In specific embodiments, heat exchangers andkettle-type reboilers may be used as the reboilers 110, 124 andcondensers 122, 132 described herein.

The heat exchangers 102, 104, 114, 118, 126 described herein may be anyof a variety of process equipment suitable for heating or cooling any ofthe streams described herein. Generally, heat exchangers 102, 104, 114,118, 126 are relatively simple devices that allow heat to be exchangedbetween two fluids without the fluids directly contacting each other. Inthe case of an air cooler, one of the fluids is atmospheric air, whichmay be forced over tubes or coils using one or more fans. The types ofheat exchangers 102, 104, 114, 118, 126 suitable for use with the carbondioxide fractionalization process 100 include shell and tube,kettle-type, air cooled, hairpin, bayonet, and plate-fin heatexchangers.

The compressor 112 and pump 128 described herein may be any of a varietyof process equipment suitable for increasing the pressure, temperature,and/or density of any of the streams described herein. Generally,compressors are associated with vapor streams and pumps are associatedwith liquid streams; however such a limitation should not be read intothe present processes as the compressors and pumps described herein maybe interchangeable based upon the specific conditions and compositionsof the streams. The types of compressors and pumps suitable for the usesdescribed herein include centrifugal, axial, positive displacement,rotary, and reciprocating compressors and pumps. Finally, the carbondioxide fractionalization process 100 may contain additional compressorsand/or pumps other than those described herein.

The mixer 116 described herein may either be a dynamic mixer or a staticmixer. Dynamic mixers are mixers that employ motion or mechanicalagitation to mix two or more streams. For example, a dynamic mixer maybe a tank with a paddle operating either in a continuous or batch mode.In contrast, static mixers are mixers that do not employ any motion ormechanical agitation to mix two or more streams. For example, a staticmixer may be a convergence of piping designed to combine two streams,such as a pipe tee. Either type of mixer may be configured with internalbaffles to promote the mixing of the feed streams.

The energy streams 300, 302, 304, 306, 308, 310, 312, 314 describedherein may be derived from any number of suitable sources. For example,heat may be added to a process stream using steam, turbine exhaust, orsome other hot fluid and a heat exchanger. Similarly, heat may beremoved from a process stream by using a refrigerant, air, or some othercold fluid and a heat exchanger. Further, electrical energy can besupplied to compressors, pumps, and other mechanical equipment toincrease the pressure or other physical properties of a fluid.Similarly, turbines, generators, or other mechanical equipment can beused to extract physical energy from a stream and optionally convert thephysical energy into electrical energy. Persons of ordinary skill in theart are aware of how to configure the processes described herein withthe required energy streams 300, 302, 304, 306, 308, 310, 312, 314. Inaddition, persons of ordinary skill in the art will appreciate that thecarbon dioxide fractionalization process 100 may contain additionalequipment, process steams, and/or energy streams other than thosedescribed herein.

The carbon dioxide fractionalization process 100 described herein hasmany advantages. One advantage is that it purifies a hydrocarbon streamused by one of the hydrocarbon sweetening processes 130 described above.Specifically, the carbon dioxide fractionalization process 100 purifiesthe hydrocarbon stream by removing some of the carbon dioxide and C₃₊from the hydrocarbon stream. The purification of the hydrocarbon streamimproves the performance of the hydrocarbon sweetening process 130 byreducing the carbon dioxide and C₃₊ loading on the hydrocarbonsweetening process 130. The reduction in loading increases theprocessing capacity for the hydrocarbon sweetening process 130, which isparticularly advantageous for existing processing facilities. Moreover,the addition of the carbon dioxide fractionalization process 100 toexisting hydrocarbon sweetening processes 130 may reduce the energyrequirements of the combined processes. Specifically, the carbon dioxidefractionalization process 100 liquefies some of the carbon dioxide andC₃₊ in the hydrocarbon feed and feeds the carbon dioxide-lean stream 234to the sweetening process 130, thereby reducing the compressionrequirements within the hydrocarbon sweetening process 130. Thereduction in compression requirements may decrease the total energyrequirements of the two processes per unit amount of hydrocarbons, e.g.Btu/SCF (British thermal units per standard cubic foot of gas). Otheradvantages will be apparent to persons of ordinary skill in the art.

EXAMPLES

In one example, a process simulation was performed using the carbondioxide fractionalization process 100 shown in FIG. 1. The simulationwas performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198)software package. The carbon dioxide fractionalization process 100separated a West Texas hydrocarbon feed containing about 63 percentcarbon dioxide into a carbon dioxide-lean stream 234 containing about 43percent carbon dioxide, a carbon dioxide-rich stream 244 containingabout 95 percent carbon dioxide, an acid gas stream 250 containing about100 percent carbon dioxide and trace amounts of other acid gases, and aheavy hydrocarbon stream containing about 99 percent C₃₊. It is notablethat the process produces 454 gallons per minute of pipeline-gradeliquefied carbon dioxide. The carbon dioxide produced by a SELEXOL®plant without this process produces a similar amount of gaseous carbondioxide, but at atmospheric pressure or at a vacuum. The compressionrequirements for such a gaseous carbon dioxide stream are large, e.g.25,000 BTU per thousand standard cubic feet (MSCF), and are generallycost prohibitive. Thus, the present process allows carbon dioxide to beeconomically recovered and reused, unlike the prior processes. Thematerial streams, their compositions, and the associated energy streamsproduced by the simulation are provided in tables 1, 2, and 3 below. Thespecified values are indicated by an asterisk (*). The physicalproperties are provided in degrees Fahrenheit (F), pounds per squareinch gauge (psig), million standard cubic feet per day (MMSCFD), poundsper hour (lb/hr), U.S. gallons per minute (USGPM), and British thermalunits per hour (Btu/hr).

TABLE 1A Material Streams Name 200 248 202 224 Vapor Fraction 1.00001.0000 1.0000 1.0000 Temperature 100.0* −15.92 99.00* 60.00* (F.)Pressure (psig) 485.3* 385.3 480.3 980.3 Molar Flow 100.0* 99.82 100.099.82 (MMSCFD) Mass Flow  3.731e+05  3.713e+05  3.731e+05  3.713e+05(lb/hr) Liquid 1176 1171 1176 1171 Volume Flow (USGPM) Heat Flow−1.305e+09 −1.316e+09 −1.305e+09 −1.315e+09 (Btu/hr)

TABLE 1B Material Streams Name 230 240 232 234 Vapor Fraction 1.00000.0000 1.0000 1.0000 Temperature −5.769 65.16 92.33 92.78 (F.) Pressure(psig) 925.3 935.3 920.3 915.3 Molar Flow 61.13 38.68 61.13 61.13(MMSCFD) Mass Flow  1.896e+05  1.817e+05  1.896e+05  1.896e+05 (lb/hr)Liquid 716.7 454.5 716.7 716.7 Volume Flow (USGPM) Heat Flow −6.242e+08−7.078e+08 −6.145e+08 −6.145e+08 (Btu/hr)

TABLE 1C Material Streams Name 244 242 218 212 Vapor Fraction   0.00000.0000 1.0000 0.0000 Temperature 72.39 55.00 123.3 264.0 (F.) Pressure(psig) 1785*    930.3 985.3* 395.3 Molar Flow 38.68 38.68 99.82 0.1832(MMSCFD) Mass Flow  1.817e+05  1.817e+05  3.713e+05 1801 (lb/hr) Liquid454.5  454.5 1171 5.233 Volume Flow (USGPM) Heat Flow −7.092e+08−7.100e+08 −1.306e+09 −1.905e+06 (Btu/hr)

TABLE 1D Material Streams Name 250 252 254 Vapor 1.0000 0.0000 0.0000Fraction Tem- (F.) 100.0* 265.2* 120.0* perature Pressure (psig) 485.3*485.3* 465.3* Molar (MMSCFD) 0.02473 0.1585 0.1585 Flow Mass (lb/hr)119.5 1682 1682 Flow Liquid (USGPM) 0.2892 4.944 4.944 Volume Flow HeatFlow (Btu/hr) −4.610e+05 −1.444e+06 −1.593e+06

TABLE 2A Stream Compositions Name 200 248 202 224 Comp Mole Frac (H2S)0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0051* 0.00510.0051 0.0051 Comp Mole Frac (CO2) 0.6308* 0.6317 0.6308 0.6317 CompMole Frac (Methane) 0.3570* 0.3577 0.3570 0.3577 Comp Mole Frac (Ethane)0.0037* 0.0037 0.0037 0.0037 Comp Mole Frac (Propane) 0.0013* 0.00130.0013 0.0013 Comp Mole Frac (i-Butane) 0.0002* 0.0002 0.0002 0.0002Comp Mole Frac (n-Butane) 0.0005* 0.0004 0.0005 0.0004 Comp Mole Frac(i-Pentane) 0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0007* 0.00000.0007 0.0000 Comp Mole Frac (n-Octane) 0.0008* 0.0000 0.0008 0.0000Comp Mole Frac (H2O) 0.0000* 0.0000 0.0000 0.0000

TABLE 2B Stream Compositions Name 230 240 232 234 Comp Mole Frac (H2S)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0083 0.00010.0083 0.0083 Comp Mole Frac (CO2) 0.4303 0.9500 0.4303 0.4303 Comp MoleFrac (Methane) 0.5568 0.0430 0.5568 0.5568 Comp Mole Frac (Ethane)0.0041 0.0031 0.0041 0.0041 Comp Mole Frac (Propane) 0.0005 0.00250.0005 0.0005 Comp Mole Frac (i-Butane) 0.0000 0.0004 0.0000 0.0000 CompMole Frac (n-Butane) 0.0000 0.0010 0.0000 0.0000 Comp Mole Frac(i-Pentane) 0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0000 0.00000.0000 0.0000 Comp Mole Frac (n-Octane) 0.0000 0.0000 0.0000 0.0000 CompMole Frac (H2O) 0.0000 0.0000 0.0000 0.0000

TABLE 2C Stream Compositions Name 244 242 218 212 Comp Mole Frac (H2S)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0001 0.00010.0051 0.0000 Comp Mole Frac (CO2) 0.9500 0.9500 0.6317 0.1350 Comp MoleFrac (Methane) 0.0430 0.0430 0.3577 0.0001 Comp Mole Frac (Ethane)0.0031 0.0031 0.0037 0.0050 Comp Mole Frac (Propane) 0.0025 0.00250.0013 0.0142 Comp Mole Frac (i-Butane) 0.0004 0.0004 0.0002 0.0078 CompMole Frac (n-Butane) 0.0010 0.0010 0.0004 0.0472 Comp Mole Frac(i-Pentane) 0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0000 0.00000.0000 0.3813 Comp Mole Frac (n-Octane) 0.0000 0.0000 0.0000 0.4094 CompMole Frac (H2O) 0.0000 0.0000 0.0000 0.0000

TABLE 2D Stream Compositions Name 250 252 254 Comp Mole Frac (H2S)0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0000 0.0000 0.0000 CompMole Frac (CO2) 1.0000 0.0000 0.0000 Comp Mole Frac (Methane) 0.00000.0001 0.0001 Comp Mole Frac (Ethane) 0.0000 0.0058 0.0058 Comp MoleFrac (Propane) 0.0000 0.0164 0.0164 Comp Mole Frac (i-Butane) 0.00000.0090 0.0090 Comp Mole Frac (n-Butane) 0.0000 0.0545 0.0545 Comp MoleFrac (i-Pentane) 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane) 0.00000.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0000 0.4408 0.4408 Comp MoleFrac (n-Octane) 0.0000 0.4733 0.4733 Comp Mole Frac (H2O) 0.0000 0.00000.0000

TABLE 3 Energy Streams Name HeatFlow (Btu/hr) 308 8.518e+06 3023.623e+05 304 1.027e+07 306 2.505e+07 314 7.719e+05 310 2.184e+06 3121.293e+07

In another example, a process simulation was performed using the carbondioxide fractionalization process 100 shown in FIG. 2. The simulationwas performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198)software package. The carbon dioxide fractionalization process 100separated a West Texas hydrocarbon feed containing about 63 percentcarbon dioxide into a carbon dioxide-lean stream 234 containing about 36percent carbon dioxide, a carbon dioxide-rich stream 244 containingabout 95 percent carbon dioxide, and a heavy hydrocarbon streamcontaining about 93 percent C₃₊. The material streams, theircompositions, and the associated energy streams produced by thesimulation are provided in tables 4, 5, and 6 below.

TABLE 4A Material Streams Name 200 204 206 222 Vapor Fraction 1.00000.8205 0.0000 1.0000 Temperature (F.) 100.0* 22.00* 22.00 34.23 Pressure(psig) 945.3* 935.3 935.3 935.3 Molar Flow (MMSCFD) 300.0* 300.0 53.85299.6 Mass Flow (lb/hr) 1.119e+06 1.119e+06 2.343e+05 1.115e+06 LiquidVolume Flow (USGPM) 3529 3529 640.1 3516 Heat Flow (Btu/hr) −3.932e+09−3.988e+09 −8.836e+08 −3.961e+09

TABLE 4B Material Streams Name 214 212 202 218 Vapor Fraction 1.00000.0000 1.0000 1.0000 Temperature (F.) −5.027 335.1 47.95 100.0* Pressure(psig) 335.3 340.3 940.3 960.3* Molar Flow (MMSCFD) 53.41 0.4397 300.053.41 Mass Flow (lb/hr) 2.299e+05 4409 1.119e+06 2.299e+05 Liquid VolumeFlow (USGPM) 627.1 12.95 3529 627.1 Heat Flow (Btu/hr) −8.582e+08−4.030e+06 −3.957e+09 −8.564e+08

TABLE 4C Material Streams Name 224 230 240 232 Vapor Fraction 1.00001.0000 0.00000 1.0000 Temperature (F.) 32.00* −20.00 61.65 −17.19Pressure (psig) 930.3 895.3 900.3 890.3 Molar Flow (MMSCFD) 299.6 161.3138.3 161.3 Mass Flow (lb/hr) 1.115e+06 4.649e+05 6.501e+05 4.649e+05Liquid Volume Flow (USGPM) 3516 1890 1626 1890 Heat Flow (Btu/hr)−3.962e+09 −1.473e+09 −2.533e+09 −1.472e+09

TABLE 4D Material Streams Name 234 244 242 220 216 Vapor Fraction 1.00000.0000  0.0000 1.0000 1.0000 Temperature (F.) 85.00* 73.48    55.00*22.00 155.2 Pressure (psig) 885.3 1785*      895.3 935.3 965.3 MolarFlow (MMSCFD) 161.3 138.3     138.3 246.2 53.41 Mass Flow (lb/hr)4.649e+05  6.501e+05 6.501e+05 8.851e+05 2.299e+05 Liquid Volume Flow(USGPM) 1890 1626       1626 2889 627.1 Heat Flow (Btu/hr) −1.446e+09−2.535e+09 −2.538e+09 −3.105e+09 −8.518e+08

TABLE 5A Stream Compositions Name 200 204 206 220 Comp Mole Frac (H2S)0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0051* 0.00510.0016 0.0051 Comp Mole Frac (CO2) 0.6308* 0.6308 0.8168 0.6316 CompMole Frac (Methane) 0.3570* 0.3570 0.1680 0.3576 Comp Mole Frac (Ethane)0.0037* 0.0037 0.0037 0.0037 Comp Mole Frac (Propane) 0.0013* 0.00130.0020 0.0013 Comp Mole Frac (i-Butane) 0.0002* 0.0002 0.0004 0.0001Comp Mole Frac (n-Butane) 0.0005* 0.0005 0.0011 0.0003 Comp Mole Frac(i-Pentane) 0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000* 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0007* 0.00070.0028 0.0002 Comp Mole Frac (n-Octane) 0.0008* 0.0008 0.0037 0.0001Comp Mole Frac (H2O) 0.0000* 0.0000 0.0000 0.0000

TABLE 5B Stream Compositions Name 214 212 202 218 Comp Mole Frac (H2S)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0016 0.00000.0051 0.0016 Comp Mole Frac (CO2) 0.8229 0.0700 0.6308 0.8229 Comp MoleFrac (Methane) 0.1693 0.0000 0.3570 0.1693 Comp Mole Frac (Ethane)0.0037 0.0000 0.0037 0.0037 Comp Mole Frac (Propane) 0.0018 0.03020.0013 0.0018 Comp Mole Frac (i-Butane) 0.0001 0.0252 0.0002 0.0001 CompMole Frac (n-Butane) 0.0003 0.0949 0.0005 0.0003 Comp Mole Frac(i-Pentane) 0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0001 0.32600.0007 0.0001 Comp Mole Frac (n-Octane) 0.0000 0.4537 0.0008 0.0000 CompMole Frac (H2O) 0.0000 0.0000 0.0000 0.0000

TABLE 5C Stream Compositions Name 224 230 240 232 Comp Mole Frac (H2S)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0051 0.00940.0000 0.0094 Comp Mole Frac (CO2) 0.6316 0.3586 0.9500 0.3586 Comp MoleFrac (Methane) 0.3576 0.6275 0.0428 0.6275 Comp Mole Frac (Ethane)0.0037 0.0041 0.0032 0.0041 Comp Mole Frac (Propane) 0.0013 0.00040.0023 0.0004 Comp Mole Frac (i-Butane) 0.0001 0.0000 0.0003 0.0000 CompMole Frac (n-Butane) 0.0003 0.0000 0.0007 0.0000 Comp Mole Frac(i-Pentane) 0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane)0.0000 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0002 0.00000.0005 0.0000 Comp Mole Frac (n-Octane) 0.0001 0.0000 0.0002 0.0000 CompMole Frac (H2O) 0.0000 0.0000 0.0000 0.0000

TABLE 5D Stream Compositions Name 234 244 242 220 216 Comp Mole Frac(H2S) 0.0000 0.0000 0.0000 0.0000 0.0000 Comp Mole Frac 0.0094 0.00000.0000 0.0059 0.0016 (Nitrogen) Comp Mole Frac (CO2) 0.3586 0.95000.9500 0.5901 0.8229 Comp Mole Frac 0.6275 0.0428 0.0428 0.3984 0.1693(Methane) Comp Mole Frac 0.0041 0.0032 0.0032 0.0037 0.0037 (Ethane)Comp Mole Frac 0.0004 0.0023 0.0023 0.0011 0.0018 (Propane) Comp MoleFrac 0.0000 0.0003 0.0003 0.0001 0.0001 (i-Butane) Comp Mole Frac 0.00000.0007 0.0007 0.0003 0.0003 (n-Butane) Comp Mole Frac 0.0000 0.00000.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.00000.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0000 0.0005 0.0005 0.00020.0001 (n-Hexane) Comp Mole Frac 0.0000 0.0002 0.0002 0.0001 0.0000(n-Octane) Comp Mole Frac (H2O) 0.0000 0.0000 0.0000 0.0000 0.0000

TABLE 6 Energy Streams Heat Flow Name (Btu/hr) 300 3.107e+07 3022.138e+07 304 6.401e+06 306 7.371e+07 308 3.014e+07 314 2.890e+06 3104.946e+06

While preferred embodiments of the invention have been shown anddescribed, modifications thereof can be made by one skilled in the artwithout departing from the spirit and teachings of the invention. Theembodiments described herein are exemplary only, and are not intended tobe limiting. Many variations and modifications of the inventiondisclosed herein are possible and are within the scope of the invention.Specifically, while the process is described in terms of a continuousprocess, it is contemplated that the process can be implemented as abatch process. In addition, where numerical ranges or limitations areexpressly stated, such express ranges or limitations should beunderstood to include iterative ranges or limitations of like magnitudefalling within the expressly stated ranges or limitations (e.g., fromabout 1 to about 10 includes, 2, 3, 4, etc.; greater than 0.10 includes0.11, 0.12, 0.13, etc.). Use of the term “optionally” with respect toany element of a claim is intended to mean that the subject element isrequired, or alternatively, is not required. Both alternatives areintended to be within the scope of the claim. Use of broader terms suchas comprises, includes, having, etc. should be understood to providesupport for narrower terms such as consisting of, consisting essentiallyof, comprised substantially of, etc. Moreover, the percentages describedherein may be mole fraction, weight fraction, or volumetric fraction.

Accordingly, the scope of protection is not limited by the descriptionset out above but is only limited by the claims which follow, that scopeincluding all equivalents of the subject matter of the claims. Each andevery claim is incorporated into the specification as an embodiment ofthe present invention. Thus, the claims are a further description andare an addition to the preferred embodiments of the present invention.The discussion of a reference in the herein is not an admission that itis prior art to the present invention, especially any reference that mayhave a publication date after the priority date of this application. Thedisclosures of all patents, patent applications, and publications citedherein are hereby incorporated by reference, to the extent that theyprovide exemplary, procedural or other details supplementary to thoseset forth herein.

What is claimed is:
 1. A process comprising: receiving a hydrocarbonfeed stream comprising carbon dioxide; separating the hydrocarbon feedstream into a light hydrocarbon stream and a heavy hydrocarbon stream;separating the light hydrocarbon stream into a carbon dioxide-richstream and a carbon dioxide-lean stream; heating the carbon dioxide-leanstream to produce a heated carbon dioxide-lean stream; and feeding theheated carbon dioxide-lean stream into a hydrocarbon sweetening process,thereby increasing the processing capacity of the hydrocarbon sweeteningprocess compared to the processing capacity of the hydrocarbonsweetening process when fed the hydrocarbon feed stream.
 2. The processof claim 1, wherein the hydrocarbon sweetening process comprises:absorbing at least some of the carbon dioxide from the heated carbondioxide-lean stream with a solvent; separating the solvent from theheated carbon dioxide-lean stream; and releasing at least some of thecarbon dioxide from the solvent by lowering the pressure of the solvent.3. The process of claim 1, wherein the hydrocarbon sweetening processcomprises separating at least some of the carbon dioxide from the heatedcarbon dioxide-lean stream using a membrane.
 4. The process of claim 1,wherein the hydrocarbon sweetening process comprises: absorbing at leastsome of the carbon dioxide from the heated carbon dioxide-lean streamwith a solvent; separating a methane-rich stream from the solvent;separating an ethane-rich stream from the solvent; and separating aheavy hydrocarbon stream from the solvent.
 5. The process of claim 1,wherein the hydrocarbon feed stream contains from about 30 molar percentto about 80 molar percent carbon dioxide.
 6. The process of claim 1,wherein the carbon dioxide-lean stream contains less than about 60 molarpercent carbon dioxide and less than about 5 molar percent C₃₊.
 7. Theprocess of claim 1, wherein the carbon dioxide-lean stream contains atleast about 95 molar percent of a combination of methane and carbondioxide.
 8. The process of claim 1, wherein the heavy hydrocarbon streamcontains at least about 90 molar percent C₃₊.
 9. The process of claim 1,wherein the carbon dioxide-rich stream contains at least about 95 molarpercent carbon dioxide.
 10. The process of claim 1, further comprisingtransferring the carbon dioxide-rich stream to a pipeline for injectioninto a subterranean formation.
 11. The process of claim 1, wherein theincrease in processing capacity of the hydrocarbon sweetening process isdirectly proportional to the decrease in carbon dioxide concentrationbetween the hydrocarbon feed stream and the heated carbon dioxide-leanstream, and the decrease in flow rate between the hydrocarbon feedstream and the heated carbon dioxide-lean stream.
 12. An apparatuscomprising: a first separator that receives a hydrocarbon feed streamcontaining carbon dioxide and produces a heavy hydrocarbon stream and alight hydrocarbon stream; a second separator that receives the lighthydrocarbon stream and produces a carbon dioxide-rich stream and acarbon dioxide-lean stream; a heat exchanger that heats the carbondioxide-lean stream to produce a heated carbon dioxide-lean stream; anda physical solvent process, a membrane process, or a carbon dioxiderecovery process that receives the heated carbon dioxide-lean stream.13. The apparatus of claim 12, wherein the first separator comprises: acolumn that receives the hydrocarbon feed stream and produces the lighthydrocarbon stream and the heavy hydrocarbon stream; and a drum thatreceives the heavy hydrocarbon stream and produces an acid gas streamand a heavy hydrocarbon stream.
 14. The apparatus of claim 12, whereinthe first separator comprises: a drum that receives the hydrocarbon feedstream and produces a light fraction and a heavy fraction; a column thatreceives the heavy fraction and produces the light hydrocarbon streamand the heavy hydrocarbon stream, the light fraction being combined withthe light hydrocarbon stream prior to the second separator.
 15. Theapparatus of claim 12, further comprising a second heat exchangerconfigured to use the carbon dioxide-lean stream to cool the lighthydrocarbon stream.
 16. The apparatus of claim 12, wherein the heatexchanger is configured to use the carbon dioxide-lean stream to coolthe hydrocarbon feed stream.
 17. A process comprising: receiving ahydrocarbon feed stream comprising carbon dioxide; cooling thehydrocarbon feed stream using a carbon dioxide-lean stream; separatingthe cooled hydrocarbon feed stream into a light hydrocarbon stream and aheavy hydrocarbon stream; compressing the light hydrocarbon stream;cooling the compressed light hydrocarbon stream using the carbondioxide-lean stream; separating the compressed light hydrocarbon streaminto a carbon dioxide-rich stream and the carbon dioxide-lean stream;heating the carbon dioxide-lean stream to produce a heated carbondioxide-lean stream; and removing at least some of the carbon dioxide inthe heated carbon dioxide-lean stream using a hydrocarbon sweeteningprocess.
 18. The process of claim 17, further comprising separating theheavy hydrocarbon stream into an acid gas stream and a heavy hydrocarbonstream.
 19. The process of claim 17, wherein separating the cooledhydrocarbon feed stream into the light hydrocarbon stream and the heavyhydrocarbon stream comprises: separating the cooled hydrocarbon feedstream into a light fraction and a heavy fraction; separating the heavyfraction into the light hydrocarbon stream and the heavy hydrocarbonstream; and combining the light fraction with the light hydrocarbonstream.
 20. The process of claim 17, wherein the hydrocarbon sweeteningprocess is a physical solvent process, a membrane process, or a carbondioxide recovery process.